WO2019015519A1 - 处理稀土精矿的方法和系统 - Google Patents

处理稀土精矿的方法和系统 Download PDF

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Publication number
WO2019015519A1
WO2019015519A1 PCT/CN2018/095309 CN2018095309W WO2019015519A1 WO 2019015519 A1 WO2019015519 A1 WO 2019015519A1 CN 2018095309 W CN2018095309 W CN 2018095309W WO 2019015519 A1 WO2019015519 A1 WO 2019015519A1
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Prior art keywords
rare earth
fluorine
outlet
inlet
earth concentrate
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PCT/CN2018/095309
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English (en)
French (fr)
Chinese (zh)
Inventor
唐建文
杜国山
羡鹏飞
邱爽
周文龙
覃波
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中国恩菲工程技术有限公司
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Application filed by 中国恩菲工程技术有限公司 filed Critical 中国恩菲工程技术有限公司
Priority to RU2019136415A priority Critical patent/RU2746867C1/ru
Priority to KR1020197033564A priority patent/KR102364012B1/ko
Priority to BR112019025160-0A priority patent/BR112019025160B1/pt
Priority to AU2018303510A priority patent/AU2018303510B2/en
Priority to JP2020517260A priority patent/JP6941229B2/ja
Publication of WO2019015519A1 publication Critical patent/WO2019015519A1/zh
Priority to ZA2019/07015A priority patent/ZA201907015B/en
Priority to US16/663,964 priority patent/US11773467B2/en

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B59/00—Obtaining rare earth metals
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • C22B1/06—Sulfating roasting
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/02—Apparatus therefor
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
    • C22B60/02—Obtaining thorium, uranium, or other actinides
    • C22B60/0291—Obtaining thorium, uranium, or other actinides obtaining thorium
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present disclosure is in the field of rare earth production, and in particular, the present disclosure relates to methods and systems for processing rare earth concentrates.
  • Baotou mixed ore [mixed ore of fluorocarbon strontium rare earth and monazite (phosphorite/phosphorite)] and bastnasite are important components of rare earth ore in China.
  • the current industrial method for treating such ore is mainly concentrated sulfuric acid roasting. The process is continuous and easy to control, and is easy to be mass-produced.
  • the strontium in the ore enters the slag in the form of strontium pyrophosphate, which causes radioactive pollution and also causes waste of strontium resources. And the recycling of fluorine and sulfur waste gas is difficult.
  • the current industrial acid hydrolysis method is mainly oxidative roasting-hydrochloric acid.
  • This method is characterized by small investment, but there are problems such as discontinuous process, difficulty in recycling strontium and fluorine in slag and wastewater, and pollution to the environment. It can be seen that the treatment of mixed ore and bastnasite in high temperature conditions is likely to cause waste of waste resources and environmental pollution of exhaust gas.
  • the present disclosure aims to solve at least one of the technical problems in the related art to some extent. To this end, it is an object of the present disclosure to provide a method and system for processing rare earth concentrates.
  • the method can treat fluorocarbon lanthanum rare earth or mixed mineral containing fluorocarbon lanthanum rare earth or monazite, has low energy consumption, can realize continuous production, can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrate.
  • the REO decomposition rate can reach 96%.
  • the present disclosure provides a method of treating a rare earth concentrate, according to an embodiment of the present disclosure, the method comprising:
  • the leaching slurry is subjected to solid-liquid separation treatment to obtain a filtrate and leaching slag, and the leaching slag is returned to the step (2) for the acid hydrolysis treatment.
  • the method for treating system concentrate according to an embodiment of the present disclosure can achieve rapid forced mixing of concentrated sulfuric acid and rare earth concentrate by arranging a stirrer in the mixing device, so that the rare earth concentrate and the concentrated sulfuric acid are sufficiently wetted, thereby avoiding the subsequent acid
  • the agglomeration phenomenon occurs during the solution process, which creates favorable conditions for the mass transfer of the acid hydrolysis process, and the water-cooled jacket on the outer wall of the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is kept constant.
  • the decomposition of the rare earth ore at high temperature can be effectively avoided, thereby realizing the recovery of the thorium resource; at the same time, in the present application, the two processes of maturation and roasting can be realized in the acid hydrolysis device, thereby significantly shortening the rare earth essence.
  • the time of the acid hydrolysis reaction, and during the acid hydrolysis process the viscosity of the internal material changes greatly, from the fluid state to the semi-dry state, and finally becomes dry, and the clinker is obtained.
  • the acid hydrolysis device can effectively cope with the above material properties. The change.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the strontium resources can be recycled and utilized to avoid the radioactive hazard of hydrazine; the leaching slag obtained after the solid-liquid separation of the leaching slurry can continue to return.
  • the acid hydrolysis treatment in the acid hydrolysis apparatus can further increase the recovery rate of ruthenium and the decomposition rate of REO. Therefore, the method has wide adaptability of raw materials, low energy consumption, and can realize continuous production, and can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrates, and the decomposition rate of REO can reach 96%.
  • the method of processing rare earth concentrate according to the above embodiment of the present disclosure may further have the following additional technical features:
  • the method before the mixing the rare earth concentrate with the concentrated sulfuric acid, the method further comprises: (5) ball milling the rare earth concentrate to obtain rare earth concentrate particles; (6) The rare earth concentrate particles are subjected to a sieving treatment to obtain a screen top material and a screen blank, and the screen material is returned to the ball milling treatment, and the screen blank is mixed with the concentrated sulfuric acid. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the above method and system for processing rare earth concentrate further comprises: (7) spraying the first fluorine-containing gas and the second fluorine-containing gas under the action of a spray liquid Treatment to obtain a fluorine-containing slurry.
  • the rare earth concentrate in step (1), has a particle size of 80-320 mesh. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the mass ratio of the rare earth concentrate to the concentrated sulfuric acid is 1: (1.2-1.5). Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • step (1) the temperature of the mixing process is no higher than 30 degrees Celsius and the time is 5-15 minutes. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the concentrated sulfuric acid has a mass concentration of not less than 93% by weight. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • step (2) the temperature of the acid hydrolysis treatment is 150-300 degrees Celsius and the time is 1-4 hours. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the initiator liquid is at least one selected from the group consisting of industrial water or a filtrate in a subsequent process. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • step (3) the time of the leaching process is 0.5-1 h. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • step (3) the mass ratio of the water to the clinker is (8-12):1. Thereby, the decomposition rate of the rare earth element oxide can be further improved.
  • the shower liquid is at least one selected from the group consisting of water and alkali.
  • the present disclosure provides a system for implementing the above method of treating a rare earth concentrate, according to an embodiment of the present disclosure, the system comprising:
  • a mixing device having a rare earth concentrate inlet, a concentrated sulfuric acid inlet, a mixed slurry outlet, and a first fluorine-containing gas outlet, and an agitator disposed in the mixing device, the mixing device being disposed on an outer wall Water-cooled jacket;
  • An acid hydrolysis device having a mixed slurry inlet, an initiator inlet, a clinker outlet, and a second fluorine-containing gas outlet, the mixed slurry inlet being connected to the mixed slurry outlet, and arranged in the acid hydrolysis device There is a stirring paddle, and a heating device is arranged on the outer wall of the acid dissolving device;
  • a leaching device having a clinker inlet, a water inlet, and a leaching slurry outlet, the clinker inlet being connected to the clinker outlet;
  • a solid-liquid separation device having a leaching slurry inlet, a filtrate outlet, and a leaching slag outlet, the leaching slurry inlet being connected to the leaching slurry outlet, the leaching slag outlet being connected to the acid hydrolysis device.
  • the system for treating rare earth concentrate by rapidly arranging a stirrer in the mixing device, rapid forced mixing of the concentrated sulfuric acid and the rare earth concentrate can be achieved, so that the rare earth concentrate and the concentrated sulfuric acid are sufficiently wetted, thereby avoiding subsequent
  • the agglomeration phenomenon occurs during the acid hydrolysis process, which creates favorable conditions for the mass transfer of the acid hydrolysis process, and the water-cooled jacket on the outer wall of the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is maintained at Within a certain range, in this way, the decomposition of the rare earth ore at high temperature can be effectively avoided, thereby realizing the recovery of the thorium resource; at the same time, in the present application, the two processes of maturation and roasting can be realized in the acid hydrolysis device, thereby significantly shortening the rare earth
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the strontium resources can be recycled and utilized to avoid the radioactive hazard of hydrazine; the leaching slag obtained after the solid-liquid separation of the leaching slurry can continue to return.
  • the acid hydrolysis treatment in the acid hydrolysis apparatus can further increase the recovery rate of ruthenium and the decomposition rate of REO.
  • the system has wide adaptability, low energy consumption, and continuous production, and can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrates, and the REO decomposition rate can reach 96%.
  • system for processing rare earth concentrate may further have the following additional technical features:
  • the system for treating a rare earth concentrate further includes: a ball milling device having a rare earth concentrate inlet and a rare earth concentrate particle outlet; a screening device having a rare earth concentrate a mineral particle inlet, a sieve upper material outlet and a sieve lower material outlet, wherein the rare earth concentrate particle inlet is connected to the rare earth concentrate particle outlet, and the sieve upper material outlet is connected to the ball milling device, and the sieve blank outlet Connected to the rare earth concentrate inlet.
  • a ball milling device having a rare earth concentrate inlet and a rare earth concentrate particle outlet
  • a screening device having a rare earth concentrate a mineral particle inlet, a sieve upper material outlet and a sieve lower material outlet, wherein the rare earth concentrate particle inlet is connected to the rare earth concentrate particle outlet, and the sieve upper material outlet is connected to the ball milling device, and the sieve blank outlet Connected to the rare earth concentrate inlet.
  • the system for treating a rare earth concentrate further includes: an exhaust gas treatment device having a fluorine-containing gas inlet, a spray liquid inlet, and a fluorine-containing slurry outlet, the fluorine-containing gas inlet And connected to the first fluorine-containing gas outlet and the second fluorine-containing gas outlet, respectively.
  • the rare earth concentrate inlet, the concentrated sulfuric acid inlet, and the first fluorine-containing gas outlet are each independently located at an upper portion of the agitator, A mixed slurry outlet is located at a lower portion of the agitator.
  • the mixed slurry inlet and the second fluorine-containing gas outlet are respectively independently located at an upper portion of the acid hydrolysis device, and the clinker outlet is located at the The lower part of the acid hydrolysis device.
  • FIG. 1 is a schematic flow chart of a method of processing a rare earth concentrate according to an embodiment of the present disclosure
  • FIG. 2 is a schematic flow chart of a method of processing rare earth concentrate according to still another embodiment of the present disclosure
  • FIG. 3 is a schematic flow chart of a method for treating rare earth concentrate according to still another embodiment of the present disclosure.
  • FIG. 4 is a schematic structural diagram of a system for carrying out a method of processing a rare earth concentrate according to an embodiment of the present disclosure
  • FIG. 5 is a schematic structural diagram of a system for carrying out a method of processing a rare earth concentrate according to still another embodiment of the present disclosure
  • FIG. 6 is a schematic diagram of a system configuration for carrying out a method of processing a rare earth concentrate according to still another embodiment of the present disclosure.
  • first and second are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated.
  • features defining “first” and “second” may include at least one of the features, either explicitly or implicitly.
  • the meaning of "a plurality” is at least two, such as two, three, etc., unless specifically defined otherwise.
  • the terms “installation”, “connected”, “connected”, “fixed”, and the like, are to be understood broadly, and may be either a fixed connection or a detachable connection, unless explicitly stated or defined otherwise. , or integrated; can be mechanical or electrical connection; can be directly connected, or indirectly connected through an intermediate medium, can be the internal communication of two elements or the interaction of two elements, unless otherwise specified Limited.
  • the specific meanings of the above terms in the present disclosure can be understood by those skilled in the art on a case-by-case basis.
  • the first feature "on” or “under” the second feature may be a direct contact of the first and second features, or the first and second features may be indirectly through an intermediate medium, unless otherwise explicitly stated and defined. contact.
  • the first feature "above”, “above” and “above” the second feature may be that the first feature is directly above or above the second feature, or merely that the first feature level is higher than the second feature.
  • the first feature “below”, “below” and “below” the second feature may be that the first feature is directly below or obliquely below the second feature, or merely that the first feature level is less than the second feature.
  • the present disclosure provides a method of processing a rare earth concentrate, according to an embodiment of the present disclosure, with reference to FIG. 1, the method comprising:
  • the rare earth concentrate is mixed with concentrated sulfuric acid to obtain a mixed slurry and a first fluorine-containing gas.
  • the mixing device is a mixture of rare earth concentrate and concentrated sulfuric acid. When mixed with acid, a small amount of CO 2 , HF and SiF 4 gas are generated, and CO 2 and HF are derived from some carbonates in the rare earth concentrate. The substance reacts with concentrated sulfuric acid and is accompanied by some solid dust in the first fluorine-containing gas.
  • the rare earth concentrate of suitable particle size is added to the mixing device through a quantitative feeder and the metered concentrated sulfuric acid according to a certain ratio, and after stirring for a certain period of time, a mixed mixed slurry is formed, and the circulating cooling water is turned on.
  • the above rare earth concentrate may be a fluorocarbon lanthanum rare earth or a Baotou mixed ore (a fluorocarbon lanthanum rare earth and a monazite).
  • the particle size of the rare earth concentrate is not particularly limited, and those skilled in the art may select according to actual needs.
  • the rare earth concentrate may have a particle diameter of 80. -320 mesh.
  • the inventors have found that if the particle size of the rare earth concentrate is too large, it is not conducive to the reaction between the rare earth concentrate and the concentrated sulfuric acid, while the small particle size can increase the contact area between the rare earth concentrate and the concentrated sulfuric acid, but the reaction is too intense, making the reaction impossible. Control, thereby not only causing excessive energy consumption in grinding, but also reducing the decomposition rate of rare earth concentrate.
  • the particle size of the rare earth concentrate proposed by the present disclosure can significantly increase the decomposition rate of the rare earth concentrate while saving energy consumption.
  • the mixing mass ratio of the rare earth concentrate to the concentrated sulfuric acid is not particularly limited, and those skilled in the art can select according to actual needs.
  • the rare earth concentrate and the rare earth concentrate The mixed mass ratio of concentrated sulfuric acid may be 1: (1.2-1.5). The inventors found that the low mass ratio of rare earth concentrate to concentrated sulfuric acid would cause insufficient reaction between rare earth concentrate and concentrated sulfuric acid, resulting in low decomposition rate of rare earth concentrate, and also caused the bismuth in rare earth concentrate to be difficult to decompose.
  • the enrichment is in the leaching slag to form radioactive slag; and if the mass ratio of the rare earth concentrate to the concentrated sulphuric acid is too high, the concentrated sulfuric acid is excessively consumed, the mixing time is prolonged, and the residual acid in the subsequent process is high. Therefore, the mixing ratio of the rare earth concentrate and the concentrated sulfuric acid proposed by the present disclosure can further increase the decomposition rate of the rare earth concentrate, and at the same time increase the mixing rate and save energy.
  • the conditions of the mixing process are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the mixing process may be no higher than 30 degrees Celsius.
  • the time can be 5-15min.
  • the inventors have found that the excessive temperature of the mixed treatment causes the rare earth concentrate to produce a local reaction in advance with the concentrated sulfuric acid, and the mixing effect is poor; the mixing time is too short to reach the condition that the rare earth concentrate is in full contact with the concentrated sulfuric acid, and the mass transfer effect is affected. Therefore, if the mixing treatment temperature is too high and the mixing time is too long or too short, the decomposition rate of the rare earth element oxide in the rare earth concentrate is lowered.
  • the mass concentration of concentrated sulfuric acid is not particularly limited, and those skilled in the art may select according to actual needs. According to a specific embodiment of the present disclosure, the mass concentration of concentrated sulfuric acid may be not lower than 93wt%. The inventors have found that the use of concentrated sulfuric acid at this concentration can significantly improve the infiltration efficiency of the rare earth concentrate, and at the same time improve the quality of the mixed slurry and thereby increase the decomposition rate of the rare earth element oxide.
  • the mixed slurry and the initiator are mixed for acid hydrolysis to obtain clinker and a second fluorine-containing gas.
  • the mixed slurry is added to the acid hydrolysis device through the mixed slurry outlet of the mixing device, and the inlet liquid inlet valve is opened, the concentrated sulfuric acid in the mixed slurry is diluted, and the acid solution is adjusted by the auxiliary heating device.
  • the acid hydrolysis reaction is completed in the acid hydrolysis device to form a bulk clinker.
  • the inventors have found that in the acid hydrolysis device, the two processes of maturation and roasting can be completed, the time for the acid hydrolysis reaction of the rare earth concentrate is significantly shortened, and in the acid hydrolysis process, the viscosity of the internal material changes greatly, and gradually changes from the fluid state. In the semi-dry state, it eventually becomes dry and clinker is obtained, and the acid hydrolysis device can effectively cope with the change of the characteristics of the above materials.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can effectively avoid concentrated sulfuric acid due to the low temperature in the whole acid hydrolysis process.
  • the decomposition of the generated sulfur-containing gas makes it possible to recycle the generated second fluorine-containing gas, and at the same time, it can effectively prevent the waste from entering the slag and causing radioactive pollution and waste of cesium resources.
  • the conditions of the acid hydrolysis treatment are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the acid hydrolysis treatment may be 150-300. Celsius, the time can be 1-4h.
  • the inventors have found that the excessive temperature of the acid hydrolysis treatment causes the concentrated sulfuric acid to decompose to produce a sulfur-containing gas, and at the same time, the bismuth in the subsequent clinker is not easily leached into the solution and remains in the leaching slag to form a radioactive solid waste; Too low and too short acid hydrolysis time will lead to low decomposition rate of rare earth element oxides; too long acid hydrolysis time can not further increase the decomposition rate of rare earth concentrates, but increase energy consumption and prolong the whole process time.
  • the temperature and time of the acid hydrolysis treatment proposed by the present disclosure can significantly increase the decomposition rate of the rare earth concentrate, increase the leaching rate of the ruthenium, and save energy.
  • the specific type of the initiating liquid is not particularly limited, and those skilled in the art may select according to actual needs.
  • the initiating liquid may be selected from an extraction process.
  • rare earth concentrate is mixed with concentrated sulfuric acid and heated to a certain temperature
  • REO, ThO 2 and the like in the concentrate react with sulfuric acid to form soluble sulfate.
  • CaF 2 , Fe 2 O 3 and the like also react to varying degrees to sulfate.
  • Rare earth sulfate, barium sulfate, iron sulfate or the like can be dissolved in an aqueous solution.
  • Fluorine enters the calcination off-gas in the form of HF or SiF 4 and can be reacted with ammonia in the presence of steam to form solid ammonium hydrogen fluoride (NH 4 HF 2 ), which is sold as a product.
  • ThO 2 +2H 2 SO 4 Th(SO 4 ) 2 +2H 2 O
  • SiO 2 +4HF SiF 4 ⁇ +2H 2 O
  • the clinker and water are mixed and subjected to a leaching treatment to obtain a leaching slurry.
  • the clinker in the acid hydrolysis device is sent to the leaching device through the clinker through the quantitative screw machine, and a certain proportion of water is added to carry out the leaching reaction. After the reaction for a period of time, the leaching slurry is formed.
  • the inventors have found that, due to the bismuth in the rare earth concentrate during the acid hydrolysis process, the bismuth citrate enters the leaching slurry during leaching, thus realizing the recycling of strontium resources and avoiding the radioactive hazard of strontium.
  • the conditions of the leaching treatment are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the leaching treatment may be normal temperature, and the time may be 0.5-1h. The inventors have found that the leaching temperature is normal temperature, and the sulphate in the clinker can be dissolved in water without heating, thereby avoiding waste of external heat source, and the appropriate leaching time can ensure complete dissolution of the sulphate.
  • the mass ratio of water to clinker is not particularly limited, and those skilled in the art can select according to actual needs.
  • S400 The leaching slurry is subjected to solid-liquid separation treatment, and the leaching slag is returned to S200 for acid hydrolysis treatment.
  • the leaching slurry is subjected to solid-liquid separation treatment to obtain a filtrate and leaching slag, and the leaching slag is returned to S200 for acid hydrolysis treatment.
  • the leaching slurry obtained by the leaching device is sent to the solid-liquid separation device for solid-liquid separation treatment, the filtrate and the leaching slag are obtained, and the leaching slag is quantitatively returned to the acid hydrolysis device in batches, and the filtrate is fed.
  • the next extraction process Thereby, the decomposition rate of the rare earth element oxide can be remarkably improved, and the recovery rate of ruthenium can be improved.
  • the method and system for processing rare earth concentrate can achieve rapid forced mixing of concentrated sulfuric acid and rare earth concentrate by arranging a stirrer in the mixing device, so that the rare earth concentrate and concentrated sulfuric acid are sufficiently wetted, thereby avoiding The agglomeration phenomenon occurs in the subsequent acid hydrolysis process, which creates favorable conditions for the mass transfer of the acid hydrolysis process, and the water-cooled jacket on the outer wall of the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is maintained.
  • the decomposition of the rare earth ore at high temperature can be effectively avoided, thereby realizing the recovery of the thorium resource; at the same time, in the present application, the two processes of maturation and roasting can be realized in the acid hydrolysis device, thereby significantly shortening
  • the time of acid hydrolysis of rare earth concentrates, and the viscosity of internal materials changes greatly during the acid hydrolysis process, gradually changing from a fluid state to a semi-dry state, eventually becoming dry, obtaining clinker, and the acid hydrolysis device can effectively cope with the above Changes in material properties.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the strontium resources can be recycled and utilized to avoid the radioactive hazard of hydrazine; the leaching slag obtained after the solid-liquid separation of the leaching slurry can continue to return.
  • the acid hydrolysis treatment in the acid hydrolysis apparatus can further increase the recovery rate of ruthenium and the decomposition rate of REO. Therefore, the method has wide adaptability of raw materials, low energy consumption, and can realize continuous production, and can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrates, and the decomposition rate of REO can reach 96%.
  • the method before the treatment of mixing the rare earth concentrate with concentrated sulfuric acid, the method further includes:
  • the rare earth concentrate is subjected to a ball milling treatment to obtain rare earth concentrate particles.
  • a ball milling treatment to obtain rare earth concentrate particles.
  • the rare earth concentrate particles obtained above are subjected to sieving treatment to obtain a sieve top material and a sieve blank, and the sieve material is returned to a ball milling treatment, and the sieve blank is mixed with concentrated sulfuric acid.
  • the decomposition rate of the rare earth element oxide can be further improved.
  • the inventors have found that by returning the sieve material having an unqualified particle size after sieving to the ball mill for ball milling, the raw material cost and time cost of the process can be significantly saved, and the sieved material obtained after sieving can be sent to Mixing with concentrated sulfuric acid in the mixing device can further increase the decomposition rate of the rare earth element oxide.
  • the size of the undersize material may be 80-320 mesh.
  • the above method and system for processing a rare earth concentrate further includes:
  • the first fluorine-containing gas and the second fluorine-containing gas are sprayed under the action of the shower liquid to obtain a fluorine-containing slurry.
  • the recycling of the fluorine-containing gas can be realized, and the problem that the exhaust gas pollutes the environment can be avoided.
  • the inventors have found that both the mixing device and the acid hydrolysis device have temperature control devices, which significantly reduce the content of impurities in the first fluorine-containing gas and the second fluorine-containing gas, so that the first fluorine-containing gas and the second fluorine-containing gas are The dust content is small.
  • the fluorine-containing gas can be directly sprayed by the spray liquid without providing a dust removing device before the spray treatment, and the fluorine-containing gas and the dust therein are dissolved in the spray liquid, and after filtering,
  • the filter residue can be returned to the acid hydrolysis unit for recycling, and the filtrate can be used to prepare a fluoride salt. It is beneficial to realize the recovery and utilization of fluorine-containing gas and avoid the problem of exhaust gas polluting the environment.
  • the specific type of the spray liquid is not particularly limited, and those skilled in the art may select according to actual needs.
  • the spray liquid may be selected from water and At least one of the alkali liquids, wherein the alkali liquid may be ammonia water.
  • the present disclosure provides a system for implementing the above method of treating a rare earth concentrate, according to an embodiment of the present disclosure, referring to FIG. 4, the system includes: a mixing device 100, an acid hydrolysis device 200, leaching device 300 and solid-liquid separation device 400.
  • the mixing device 100 has a rare earth concentrate inlet 101, a concentrated sulfuric acid inlet 102, a mixed slurry outlet 103, and a first fluorine-containing gas outlet 104, and a stirrer 11 is disposed in the mixing device, the mixing device A water-cooling jacket 12 is disposed on the outer wall and is adapted to mix the rare earth concentrate with concentrated sulfuric acid to obtain a mixed slurry and a first fluorine-containing gas.
  • the mixing device is a mixture of rare earth concentrate and concentrated sulfuric acid. When mixed with acid, a small amount of CO 2 , HF and SiF 4 gas are generated, and CO 2 and HF are derived from some carbonates in the rare earth concentrate.
  • the substance reacts with concentrated sulfuric acid and is accompanied by some solid dust in the first fluorine-containing gas.
  • the rare earth concentrate of suitable particle size is added to the mixing device through a quantitative feeder and the metered concentrated sulfuric acid according to a certain ratio, and after stirring for a certain period of time, a mixed mixed slurry is formed, and the circulating cooling water is turned on. , control the temperature inside the mixing device within a certain range.
  • the inventors have found that by arranging the agitator in the mixing device, the rapid forced mixing of the concentrated sulfuric acid and the rare earth concentrate can be achieved, so that the rare earth concentrate and the concentrated sulfuric acid are fully wetted, thereby avoiding the agglomeration phenomenon in the subsequent acid hydrolysis process.
  • the favorable conditions for the mass transfer of the acid hydrolysis process are created.
  • the water-cooled jacket in the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is kept within a certain range.
  • the above-mentioned rare earth concentrate is not particularly limited, and may be, for example, a fluorocarbon lanthanum rare earth or a Baotou mixed ore (a fluorocarbon lanthanum rare earth and a monazite); the concentrated sulfuric acid can be pumped to a mixture by metering.
  • the agitator in the mixing device is not particularly limited, and those skilled in the art can select according to actual needs, for example, it can be a double-layer stirring paddle, that is, two layers are arranged on the stirring shaft, and can be used for rare earth. Intense mixing of concentrate with concentrated sulfuric acid.
  • the rare earth concentrate inlet 101, the concentrated sulfuric acid inlet 102, and the first fluorine-containing gas outlet 104 are independently located at the upper portion of the agitator 11, respectively, and the mixed slurry outlet 103 is located at the agitator.
  • the particle size of the rare earth concentrate is not particularly limited, and those skilled in the art may select according to actual needs.
  • the particle size of the rare earth concentrate may be 80-320 mesh. The inventors have found that if the particle size of the rare earth concentrate is too large, it is not conducive to the reaction between the rare earth concentrate and the concentrated sulfuric acid, while the small particle size can increase the contact area between the rare earth concentrate and the concentrated sulfuric acid, but the reaction is too intense, making the reaction impossible. Control, thereby not only causing excessive energy consumption in grinding, but also reducing the decomposition rate of rare earth concentrate.
  • the particle size of the rare earth concentrate proposed by the present disclosure can significantly increase the decomposition rate of the rare earth concentrate while saving energy consumption.
  • the mixing mass ratio of the rare earth concentrate to the concentrated sulfuric acid is not particularly limited, and those skilled in the art can select according to actual needs.
  • the rare earth concentrate and the rare earth concentrate The mixed mass ratio of concentrated sulfuric acid may be 1: (1.2-1.5). The inventors found that the low mass ratio of rare earth concentrate to concentrated sulfuric acid would cause insufficient reaction between rare earth concentrate and concentrated sulfuric acid, resulting in low decomposition rate of rare earth concentrate, and also caused the bismuth in rare earth concentrate to be difficult to decompose.
  • the enrichment is in the leaching slag to form radioactive slag; and if the mass ratio of the rare earth concentrate to the concentrated sulphuric acid is too high, the concentrated sulfuric acid is excessively consumed, the mixing time is prolonged, and the residual acid in the subsequent process is high. Therefore, the mixing ratio of the rare earth concentrate and the concentrated sulfuric acid proposed by the present disclosure can further increase the decomposition rate of the rare earth concentrate, and at the same time increase the mixing rate and save energy.
  • the conditions of the mixing process are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the mixing process may be no higher than 30 degrees Celsius.
  • the time can be 5-15min.
  • the inventors have found that the excessive temperature of the mixed treatment causes the rare earth concentrate to produce a local reaction in advance with the concentrated sulfuric acid, and the mixing effect is poor; the mixing time is too short to reach the condition that the rare earth concentrate is in full contact with the concentrated sulfuric acid, and the mass transfer effect is affected. Therefore, if the mixing treatment temperature is too high and the mixing time is too long or too short, the decomposition rate of the rare earth element oxide in the rare earth concentrate is lowered.
  • the mass concentration of concentrated sulfuric acid is not particularly limited, and those skilled in the art may select according to actual needs. According to a specific embodiment of the present disclosure, the mass concentration of concentrated sulfuric acid may be not lower than 93wt%. The inventors have found that the use of concentrated sulfuric acid at this concentration can significantly improve the infiltration efficiency of the rare earth concentrate, and at the same time improve the quality of the mixed slurry and thereby increase the decomposition rate of the rare earth element oxide.
  • the acid hydrolysis device 200 has a mixed slurry inlet 201, an initiator liquid inlet 202, a clinker outlet 203, and a second fluorine-containing gas outlet 204, and the mixed slurry inlet 201 is connected to the mixed slurry outlet 103, and the acid hydrolysis device
  • a stirring paddle 21 is disposed in the 200
  • a heating device 22 is disposed on the outer wall of the acid hydrolysis device, and is adapted to mix the mixed slurry and the initiator liquid for acid hydrolysis treatment to obtain clinker and a second fluorine-containing gas.
  • the mixed slurry is added to the acid hydrolysis device through the mixed slurry outlet of the mixing device, and the inlet liquid inlet valve is opened, the concentrated sulfuric acid in the mixed slurry is diluted, and the acid solution is adjusted by the auxiliary heating device.
  • the acid hydrolysis reaction is completed in the acid hydrolysis device to form a bulk clinker.
  • the inventors have found that in the acid hydrolysis device, the two processes of maturation and roasting can be completed, the time for the acid hydrolysis reaction of the rare earth concentrate is significantly shortened, and in the acid hydrolysis process, the viscosity of the internal material changes greatly, and gradually changes from the fluid state.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can effectively avoid concentrated sulfuric acid due to the low temperature in the whole acid hydrolysis process.
  • the decomposition of the generated sulfur-containing gas makes it possible to recycle the generated second fluorine-containing gas, and at the same time, it can effectively prevent the waste from entering the slag and causing radioactive pollution and waste of cesium resources.
  • the above-mentioned acid hydrolysis device is not particularly limited, and those skilled in the art may select according to actual needs, for example, may be a horizontal reactor, and the stirring paddle may be a spiral type side-by-side arrangement of agitating paddles, a heating device.
  • the heating method can be electric heating or steam heating.
  • the mixed slurry inlet 201 and the second fluorine-containing gas outlet 204 are independently located at the upper portion of the acid hydrolysis device 200, respectively, and the clinker outlet 203 is located at the lower portion of the acid hydrolysis device 200.
  • the conditions of the acid hydrolysis treatment are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the acid hydrolysis treatment may be 150- 300 degrees Celsius, the time can be 1-4h.
  • the inventors have found that the excessive temperature of the acid hydrolysis treatment causes the concentrated sulfuric acid to decompose to produce a sulfur-containing gas, and at the same time, the bismuth in the subsequent clinker is not easily leached into the solution and remains in the leaching slag to form a radioactive solid waste; Too low and too short acid hydrolysis time will lead to low decomposition rate of rare earth element oxides; too long acid hydrolysis time can not further increase the decomposition rate of rare earth concentrates, but increase energy consumption and prolong the whole process time.
  • the temperature and time of the acid hydrolysis treatment proposed by the present disclosure can significantly increase the decomposition rate of the rare earth concentrate, increase the leaching rate of the ruthenium, and save energy.
  • the specific type of the initiator liquid is not particularly limited, and those skilled in the art may select according to actual needs.
  • the initiator liquid may be selected from an extraction process. A waste acid or a type of industrial water. The inventors have found that the acid hydrolysis reaction needs to reach a certain temperature before the use of the initiator liquid can dilute the exothermic heat of the concentrated sulfuric acid, increase the temperature of the mixed slurry, and promote the progress of the acid hydrolysis reaction, so that the dilution heat can be utilized to reduce the external heat source. Supply.
  • rare earth concentrate is mixed with concentrated sulfuric acid and heated to a certain temperature
  • REO, ThO 2 and the like in the concentrate react with sulfuric acid to form soluble sulfate.
  • CaF 2 , Fe 2 O 3 and the like also react to varying degrees to sulfate.
  • Rare earth sulfate, barium sulfate, iron sulfate or the like can be dissolved in an aqueous solution.
  • Fluorine enters the calcination off-gas in the form of HF or SiF 4 and can be reacted with ammonia in the presence of steam to form solid ammonium hydrogen fluoride (NH 4 HF 2 ), which is sold as a product.
  • ThO 2 +2H 2 SO 4 Th(SO 4 ) 2 +2H 2 O
  • SiO 2 +4HF SiF 4 ⁇ +2H 2 O
  • the leaching device 300 has a clinker inlet 301, a water inlet 302, and a leaching slurry outlet 303, and the clinker inlet 301 is connected to the clinker outlet 203 and is adapted to mix the clinker and water for leaching treatment, In order to obtain a leaching slurry.
  • the clinker in the acid hydrolysis device is sent to the leaching device through the clinker through the quantitative screw machine, and a certain proportion of water is added to carry out the leaching reaction. After the reaction for a period of time, the leaching slurry is formed.
  • the inventors have found that, due to the bismuth in the rare earth concentrate during the acid hydrolysis process, the bismuth citrate enters the leaching slurry during leaching, thus realizing the recycling of strontium resources and avoiding the radioactive hazard of strontium.
  • the conditions of the leaching treatment are not particularly limited, and those skilled in the art may select according to actual needs.
  • the temperature of the leaching treatment may be normal temperature, and the time may be 0.5-1h. The inventors have found that the leaching temperature is normal temperature, and the sulphate in the clinker can be dissolved in water without heating, thereby avoiding waste of external heat source, and the appropriate leaching time can ensure complete dissolution of the sulphate.
  • the mass ratio of water to clinker is not particularly limited, and those skilled in the art can select according to actual needs.
  • the solid-liquid separation device 400 has a leaching slurry inlet 401, a filtrate outlet 402, and a leaching slag outlet 403, and the leaching slurry inlet 401 is connected to the leaching slurry outlet 303, and the leaching slag outlet 403 is connected to the acid eliminating device 200. And suitable for the solid-liquid separation treatment of the leach slurry to obtain the filtrate and the leach residue, and return the leach residue to the acid hydrolysis device for acid hydrolysis treatment.
  • the leaching slurry obtained by the leaching device is sent to the solid-liquid separation device for solid-liquid separation treatment, the filtrate and the leaching slag are obtained, and the leaching slag is quantitatively returned to the acid hydrolysis device in batches, and the filtrate is fed.
  • the next extraction process Thereby, the decomposition rate of the rare earth element oxide can be remarkably improved, and the recovery rate of ruthenium can be improved.
  • the system for treating rare earth concentrate can realize rapid forced mixing of concentrated sulfuric acid and rare earth concentrate by arranging a stirrer in the mixing device, so that the rare earth concentrate and the concentrated sulfuric acid are sufficiently wetted, thereby avoiding the subsequent acid
  • the agglomeration phenomenon occurs during the solution process, which creates favorable conditions for the mass transfer of the acid hydrolysis process, and the water-cooled jacket on the outer wall of the mixing device can cool the mixing device through the circulating water, so that the temperature inside the mixing device is kept constant.
  • the decomposition of the rare earth ore at high temperature can be effectively avoided, thereby realizing the recovery of the thorium resource; at the same time, in the present application, the two processes of maturation and roasting can be realized in the acid hydrolysis device, thereby significantly shortening the rare earth essence.
  • the time of the acid hydrolysis reaction, and during the acid hydrolysis process the viscosity of the internal material changes greatly, from the fluid state to the semi-dry state, and finally becomes dry, and the clinker is obtained.
  • the acid hydrolysis device can effectively cope with the above material properties. The change.
  • the stirring paddle in the acid hydrolysis device can accelerate the progress of the acid hydrolysis reaction, and the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the heating device on the outer wall of the acid hydrolysis device can provide a suitable temperature for the acid hydrolysis reaction, and can further avoid the enthalpy due to the low temperature during the entire acid hydrolysis process.
  • the strontium resources can be recycled and utilized to avoid the radioactive hazard of hydrazine; the leaching slag obtained after the solid-liquid separation of the leaching slurry can continue to return.
  • the acid hydrolysis treatment in the acid hydrolysis apparatus can further increase the recovery rate of ruthenium and the decomposition rate of REO.
  • the system has wide adaptability, low energy consumption, and continuous production, and can effectively recover strontium resources, and significantly improve the decomposition rate of rare earth concentrates, and the REO decomposition rate can reach 96%.
  • the above-described system for processing rare earth concentrate further includes: a ball milling device 500 and a screening device 600.
  • the ball milling apparatus 500 has a rare earth concentrate inlet 501 and a rare earth concentrate particle outlet 502, and is adapted to perform ball milling treatment on the rare earth concentrate before the rare earth concentrate is mixed with the concentrated sulfuric acid to obtain a rare earth. Concentrate particles. Thereby, it is advantageous to increase the decomposition rate of the rare earth element oxide.
  • the screening device 600 has a rare earth concentrate particle inlet 601, a screen upper material outlet 602, and a sieve lower material outlet 603, and the rare earth concentrate particle inlet 601 is connected to the rare earth concentrate particle outlet 502.
  • 602 is connected to the ball milling device 500
  • the undersize outlet 603 is connected to the rare earth concentrate inlet 101, and is adapted to sieve the rare earth concentrate particles obtained above to obtain the sieve material and the sieve material, and to sieve the sieve.
  • the material is returned to the ball milling treatment, and the sieve blank is mixed with concentrated sulfuric acid.
  • the inventors have found that by returning the sieve material having an unqualified particle size after sieving to the ball mill for ball milling, the raw material cost and time cost of the process can be significantly saved, and the sieved material obtained after sieving can be sent to Mixing with concentrated sulfuric acid in the mixing device can further increase the decomposition rate of the rare earth element oxide.
  • the screen discharge outlet of the screening device can be connected to the rare earth concentrate inlet of the above mixing device through a metering device.
  • the size of the undersize material may be 80-320 mesh.
  • the above-described system for processing rare earth concentrate further includes: an exhaust gas treatment device 700.
  • the exhaust gas treatment device 700 has a fluorine-containing gas inlet 701, a spray liquid inlet 702, a fluorine-containing slurry outlet 703, and a fluorine-containing gas inlet 701, respectively, and a first fluorine-containing gas outlet 104 and a second fluorine-containing gas outlet.
  • the 204 is connected and adapted to spray the first fluorine-containing gas and the second fluorine-containing gas under the action of the spray liquid to obtain a fluorine-containing slurry.
  • both the mixing device and the acid hydrolysis device have temperature control devices, which significantly reduce the content of impurities in the first fluorine-containing gas and the second fluorine-containing gas, so that the first fluorine-containing gas and the second fluorine-containing gas are The dust content is small.
  • the fluorine-containing gas can be directly sprayed by the spray liquid without providing a dust removing device before the spray treatment, and the fluorine-containing gas and the dust therein are dissolved in the spray liquid, and after filtering,
  • the filter residue can be returned to the acid hydrolysis device for recycling, and the filtrate can be used for preparing the fluorine salt, which is beneficial to the recovery and utilization of the fluorine-containing gas, and avoids the problem that the exhaust gas pollutes the environment.
  • the specific type of the spray liquid is not particularly limited, and those skilled in the art may select according to actual needs.
  • the spray liquid may be selected from water and At least one of the alkali liquids, wherein the alkali liquid may be ammonia water.
  • the fluorocarbon lanthanum rare earth ore is ball milled by a ball mill and sieved to obtain fluorocarbon cerium rare earth concentrate particles with a particle size of 80-320 mesh; the fluorocarbon slag rare earth concentrate is metered and then pre-measured.
  • the mixing device with 98wt% concentrated sulfuric acid the mass ratio of concentrated sulfuric acid to fluorocarbon cerium rare earth concentrate particles is 1.4:1, the circulating cooling water of the mixing device is turned on, and the temperature in the mixing device is controlled to be less than 30 degrees Celsius.
  • the loose clinker is quantitatively sent to the leaching device through the clinker outlet of the acid hydrolysis device, and in the leaching device, the water and the clinker are metered according to the mass ratio of 8:1.
  • Dip The tank is mechanically stirred for 1 hour to form a leaching slurry, and then the leaching slurry is pumped to a plate and frame filter press to obtain a filtrate and a leaching slag.
  • the leaching slag rate is 8 wt%, and the chemical composition of the leaching slag is analyzed, and the leaching slag is analyzed.
  • the aliquots are returned to the acid hydrolysis unit in batches, and the leachate is sent to the next extraction step.
  • the rare earth REO (rare earth element oxide) decomposition rate of the present embodiment is 95.18%, and the first fluorine-containing gas and the second fluorine-containing gas are recovered and utilized by the tail gas absorption tower.
  • the fluorocarbon lanthanum rare earth ore is ball milled by a ball mill and sieved to obtain fluorocarbon cerium rare earth concentrate particles with a particle size of 80-320 mesh; the fluorocarbon lanthanum rare earth concentrate particles are metered and put into pre-measurement
  • the mixing device with 98wt% concentrated sulfuric acid the mass ratio of concentrated sulfuric acid to fluorocarbon cerium rare earth concentrate particles is 1.5:1
  • the circulating cooling water of the mixing device is turned on, and the temperature in the mixing device is controlled to be less than 30 degrees Celsius, fully Stir for 8min to form a mixed slurry with uniform acid mixing, and at the same time produce a first fluorine-containing gas; then discharge the mixed slurry through the mixed slurry outlet of the mixing device, add to the acid hydrolysis device, and open the inlet liquid (waste acid) inlet valve Diluting the concentrated sulfuric acid in the mixed slurry, releasing the heat, and adjusting the temperature in the acid hydrolysis device through the auxiliary heating
  • the leaching slag rate is 6.3wt%, analyzing the chemical composition of the leaching slag, and leaching the upper leaching
  • the slag is returned to the acid hydrolysis unit in batches, and the leachate is sent to the next extraction step.
  • the rare earth REO (rare earth element oxide) decomposition rate of the present embodiment is 96%, and the first fluorine-containing gas and the second fluorine-containing gas are recovered and utilized by the tail gas absorption tower.
  • the mixed ore containing fluorocarbon lanthanum rare earth or monazite having a particle size of 80-320 mesh is metered into a mixing device pre-metered with 98 wt% concentrated sulfuric acid, and the mass ratio of concentrated sulfuric acid to mixed ore is 1.5. :1, the circulating cooling water of the mixing device is turned on, the temperature in the mixing device is controlled to be less than 30 degrees Celsius, and the mixture is stirred for 10 minutes to form a mixed slurry with uniform acid mixing, and the first fluorine-containing gas is generated; and the mixed slurry is mixed.
  • the mixed slurry outlet of the device is discharged, added to the acid hydrolysis device, the inlet liquid (mixture containing industrial water and waste acid) is opened, the concentrated sulfuric acid in the mixed slurry is diluted, the heat is released, and the auxiliary device is assisted by the acid hydrolysis device.
  • the clinker outlet is quantitatively fed to the leaching device.
  • the water and clinker are metered according to the mass ratio of 12:1, and then placed in a leaching tank, mechanically stirred for 1 hour to form a leaching slurry, and then the leaching slurry is pumped to The plate and frame filter press is filter-filtered to obtain the filtrate and the leaching slag, and the leaching slag rate is 6.8 wt%.
  • the chemical composition of the leaching slag is analyzed, and the upper leaching slag is quantitatively returned to the acid hydrolysis device in batches, and the leaching solution is sent to the next stage extraction. Process.
  • the rare earth REO (rare earth element oxide) decomposition rate of the present embodiment is 96%, and the first fluorine-containing gas and the second fluorine-containing gas are recovered and utilized by the tail gas absorption tower.
  • the mixed ore containing fluorocarbon lanthanum rare earth or monazite having a particle size of 80-320 mesh is metered into a mixing device pre-metered with 98 wt% concentrated sulfuric acid, and the mass ratio of concentrated sulfuric acid to mixed ore is 1.4.
  • the internal temperature is stirred at 100 ° C for 30 min, followed by acid hydrolysis at 280 ° C for 2 h to form a loose clinker, while producing a second fluorine-containing gas; the loose clinker is quantitatively fed through the clinker outlet of the acid hydrolysis device
  • the water and clinker are metered in a mass ratio of 10:1, placed in a leaching tank, mechanically stirred for 1 hour to form a leaching slurry, and the leaching slurry is pumped to a plate and frame filter press for pressure filtration. Too leaching residue and the filtrate, the residue leaching residue was 7.2wt%, the chemical composition analysis of leach residue, the leach residue quantitatively batches return means acidolysis, and the lower section of the extraction liquid into the leaching step.
  • the rare earth REO (rare earth element oxide) decomposition rate of the present embodiment is 96%, and the first fluorine-containing gas and the second fluorine-containing gas are recovered and utilized by the tail gas absorption tower.
PCT/CN2018/095309 2017-07-17 2018-07-11 处理稀土精矿的方法和系统 WO2019015519A1 (zh)

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BR112019025160-0A BR112019025160B1 (pt) 2017-07-17 2018-07-11 Método para processar um minério concentrado de terras raras e sistema para realizar um método para processar um minério concentrado de terras raras
AU2018303510A AU2018303510B2 (en) 2017-07-17 2018-07-11 Method and system for treatment of rare earth concentrate
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ZA2019/07015A ZA201907015B (en) 2017-07-17 2019-10-24 Method and system for treatment of rare earth concentrate
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Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107475542B (zh) * 2017-07-17 2021-03-16 中国恩菲工程技术有限公司 处理稀土精矿的方法
CN109022838B (zh) * 2018-09-14 2020-03-06 包头稀土研究院 含氟的稀土矿物颗粒的处理方法
CN109439931A (zh) * 2018-12-03 2019-03-08 包头稀土研究院 一种芒廷帕斯稀土矿资源综合利用的方法
CN109371239B (zh) * 2018-12-03 2021-03-19 包头稀土研究院 一种处理含稀土的低品位萤石矿的方法
CN110252095A (zh) * 2019-07-26 2019-09-20 李明东 一种浓硫酸分解稀土精矿产生的酸性废气的处理方法
CN111270092B (zh) * 2020-02-07 2022-08-05 包头稀土研究院 分解混合稀土矿的方法
CN111285332B (zh) * 2020-02-19 2023-03-28 包头稀土研究院 分解含氟稀土矿物和回收氢氟酸的一体化方法
CN113373326B (zh) * 2020-03-09 2022-10-04 有研稀土新材料股份有限公司 一种制备纯净硫酸稀土溶液的方法
CN111334662B (zh) * 2020-04-10 2021-12-14 包头稀土研究院 稀土精矿的分解方法
CN114107668B (zh) * 2021-11-10 2023-11-17 北京工业大学 一种机械活化强化浸出废弃抛光液中稀土的方法
CN115232960B (zh) * 2022-07-22 2023-12-12 包头稀土研究院 混合稀土精矿的处理方法及石英的用途

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1667139A (zh) * 2004-03-08 2005-09-14 中国有色工程设计研究总院 一种混合型稀土精矿分解方法
CN102031363A (zh) * 2011-01-06 2011-04-27 中冶东方工程技术有限公司 一种稀土精矿多级焙烧方法及其设备
JP2017014605A (ja) * 2015-07-06 2017-01-19 三菱マテリアル株式会社 希土類元素の回収方法
CN107267784A (zh) * 2017-07-17 2017-10-20 中国恩菲工程技术有限公司 处理稀土精矿的系统
CN107475542A (zh) * 2017-07-17 2017-12-15 中国恩菲工程技术有限公司 处理稀土精矿的方法
CN206902214U (zh) * 2017-07-17 2018-01-19 中国恩菲工程技术有限公司 处理稀土精矿的系统

Family Cites Families (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2705102B1 (fr) * 1993-05-12 1995-08-11 Rhone Poulenc Chimie Procede de traitement de compositions contenant des metaux precieux et autres elements de valeur en vue de leur recuperation.
US7282187B1 (en) * 1996-03-26 2007-10-16 Caboi Corporation Recovery of metal values
US5787332A (en) * 1996-09-26 1998-07-28 Fansteel Inc. Process for recovering tantalum and/or niobium compounds from composites containing a variety of metal compounds
RU2242528C2 (ru) * 2001-07-30 2004-12-20 Открытое акционерное общество "Ульбинский металлургический завод" Способ вскрытия монацитового концентрата
CN1173050C (zh) * 2002-09-25 2004-10-27 包头稀土研究院 稀土精矿浓硫酸低温焙烧分解工艺
WO2009021389A1 (fr) * 2007-08-10 2009-02-19 Grirem Advanced Materials Co., Ltd. Procédé de fusion d'un minerai des terres rares de type monazite riche en fe
CN101363079A (zh) * 2007-08-10 2009-02-11 有研稀土新材料股份有限公司 一种富铁独居石稀土矿的冶炼方法
CN101633981B (zh) * 2009-08-28 2011-09-14 攀钢集团钢铁钒钛股份有限公司 含钛物料的酸解方法及钛白粉的制备方法
FR2970265B1 (fr) * 2011-01-06 2013-02-08 Areva Nc Mise en solution et recuperation d'au moins un element nb, ta et d'au moins un autre element u, terres rares a partir de minerais et concentres
JP6105053B2 (ja) * 2012-05-04 2017-03-29 ヴァーレ、ソシエダージ、アノニマＶａｌｅ Ｓ．Ａ． 希土類抽出のシステムおよび方法
CN103074504A (zh) * 2012-09-29 2013-05-01 内蒙古机电职业技术学院 一种电加热内热法分解混合型稀土精矿的方法及其电热分解槽
CN103014359B (zh) * 2012-11-27 2014-03-19 益阳鸿源稀土有限责任公司 独居石渣的分离回收方法
CN102978392A (zh) * 2012-12-06 2013-03-20 内蒙古科技大学 一种微波辅助稀土精矿低温酸浸方法
RU2549412C1 (ru) * 2013-10-14 2015-04-27 Федеральное государственное бюджетное образовательное учреждение высшего профессионального образования "Национальный исследовательский Томский политехнический университет" Способ переработки монацитового концентрата
US10597754B2 (en) * 2014-05-15 2020-03-24 Vale S.A. System and process for selective rare earth extraction with sulphur recovery
CN104962762A (zh) * 2015-07-22 2015-10-07 中国恩菲工程技术有限公司 氟碳铈精矿的处理方法
CN104946887A (zh) * 2015-07-22 2015-09-30 中国恩菲工程技术有限公司 氟碳铈精矿的处理方法
CN105568006A (zh) * 2015-12-31 2016-05-11 包头稀土研究院 一种浓硫酸清洁冶炼混合稀土精矿的方法
CN105970006A (zh) * 2016-07-07 2016-09-28 攀钢集团攀枝花钢铁研究院有限公司 高氧化铁钛精矿制备钛白粉的方法
CN106636626A (zh) * 2016-12-13 2017-05-10 江苏省冶金设计院有限公司 一种处理稀土精矿的系统和方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1667139A (zh) * 2004-03-08 2005-09-14 中国有色工程设计研究总院 一种混合型稀土精矿分解方法
CN102031363A (zh) * 2011-01-06 2011-04-27 中冶东方工程技术有限公司 一种稀土精矿多级焙烧方法及其设备
JP2017014605A (ja) * 2015-07-06 2017-01-19 三菱マテリアル株式会社 希土類元素の回収方法
CN107267784A (zh) * 2017-07-17 2017-10-20 中国恩菲工程技术有限公司 处理稀土精矿的系统
CN107475542A (zh) * 2017-07-17 2017-12-15 中国恩菲工程技术有限公司 处理稀土精矿的方法
CN206902214U (zh) * 2017-07-17 2018-01-19 中国恩菲工程技术有限公司 处理稀土精矿的系统

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